Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J35/00—Catalysts, in general, characterised by their form or physical properties
  • B01J35/19—Catalysts containing parts with different compositions
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
  • B01D53/34—Chemical or biological purification of waste gases
  • B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
  • B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
  • B01D53/9404—Removing only nitrogen compounds
  • B01D53/9409—Nitrogen oxides
  • B01D53/9413—Processes characterised by a specific catalyst
  • B01D53/9418—Processes characterised by a specific catalyst for removing nitrogen oxides by selective catalytic reduction [SCR] using a reducing agent in a lean exhaust gas
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/48—Silver or gold
  • B01J23/50—Silver
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
  • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2251/00—Reactants
  • B01D2251/20—Reductants
  • B01D2251/208—Hydrocarbons
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2251/00—Reactants
  • B01D2251/20—Reductants
  • B01D2251/21—Organic compounds not provided for in groups B01D2251/206 or B01D2251/208
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/10—Noble metals or compounds thereof
  • B01D2255/102—Platinum group metals
  • B01D2255/1023—Palladium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/10—Noble metals or compounds thereof
  • B01D2255/104—Silver
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/20—Metals or compounds thereof
  • B01D2255/206—Rare earth metals
  • B01D2255/2063—Lanthanum
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/20—Metals or compounds thereof
  • B01D2255/207—Transition metals
  • B01D2255/20753—Nickel
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/20—Metals or compounds thereof
  • B01D2255/207—Transition metals
  • B01D2255/20761—Copper
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2255/00—Catalysts
  • B01D2255/90—Physical characteristics of catalysts
  • B01D2255/92—Dimensions
  • B01D2255/9207—Specific surface

Definitions

• the present invention relates to an exhaust gas cleaner for effectively removing nitrogen oxides by reduction from an exhaust gas containing nitrogen oxides and an excess amount of oxygen, and a method for cleaning an exhaust gas with such an exhaust gas cleaner.
• Various exhaust gases discharged from internal combustion engines such as automobile engines, etc., combustion apparatuses installed in factories, home fan heaters, etc. contain nitrogen oxides such as nitrogen monoxide and nitrogen dioxide together with an excess amount of oxygen.
• the term "containing an excess amount of oxygen” means that the oxygen content is larger than its stoichiometric amount relative to unburned components such as carbon monoxide, hydrogen, hydrocarbons in the exhaust gas.
• nitrogen oxides NOx
• the nitrogen oxides are one of the causes of acid rain, posing a serious problem of environmental pollution. For these reasons, various methods have been proposed to remove nitrogen oxides from exhaust gases emitted from various combustion equipment.
• ammonia is introduced into an exhaust gas, whereby nitrogen oxides in the exhaust gas are catalytically and selectively reduced (selective catalytic reduction).
• an object of the present invention is to provide an exhaust gas cleaner and a method capable of efficiently removing nitrogen oxides by reduction from an exhaust gas containing nitrogen oxides, sulfur oxides, moisture and oxygen in an amount larger than the stoichiometric amount relative to unburned components such as carbon monoxide, hydrogen, hydrocarbons, etc., which is discharged from stationary combustion apparatuses, gasoline engines operated under oxygen excess conditions, and diesel engines.
• nitrogen oxides may effectively be reduced in the presence of such nitrogen-containing compounds and aldehydes on a catalyst carrying an Nicomponent, a catalyst carrying two or more of Ag component, Cucomponent and Ni component, or a mixed catalyst of two or more of Ag catalyst, Cu catalyst and Ni catalyst, and (3) hydrocarbons, carbon monoxide and soluble organic fraction (SOF) may effectively be oxidized on a catalyst carrying a noble metal with or without a base metal.
• SOF carbon monoxide and soluble organic fraction
• an exhaust gas cleaner which comprises (1) a first catalyst comprising a first porous inorganic oxide supporting 0.2-15 weight % of at least one Ag component selected from Ag and Ag compounds; (2) a second catalyst comprising a second inorganic oxide supporting 1-30 weight %of an Ni component or 1-30 weight %of two or more of an Ag component, Cu component and Ni component, and optionally at least one component selected from 5 weight %or less of one or more of an alkali metal component and a rare earth component and 3 0 weight %or less of a base metal component, said Ni component being selected from Ni and Ni compounds, said Ag component being selected from Ag and Ag compounds, said Cu component being selected from Cu and Cu compounds, said alkali metal component being selected from alkali metal elements and oxides thereof, said rare earth component being selected from rare earth elements and oxides thereof, and said base metal component being selected from oxides of W, V, Mo, Mn, Nb and Ta; and optionally (3) a third catalyst comprising a third
• an exhaust gas cleaner which comprises (1) a first catalyst comprising a first porous inorganic oxide supporting 0.2-15 weight %of at least one Ag component selected from Ag and Ag compounds; (2) a second catalyst comprising a second inorganic oxide supporting 0.5-30 weight % of an Ni component alone or in combination with 0.5-30 weight %of a Cu component, and optionally at least one component selected from 5 weight % or less of one or more of an alkali metal component and a rare earth component and 30 weight %or less of a base metal component, said Ni component being selected from Ni and Ni compounds, said Cu component being selected from Cu and Cu compounds, said alkali metal component being selected from alkali metal elements and oxides thereof, said rare earth component being selected from rare earth elements and oxides thereof, and said base metal component being selected from oxides of W, V, Mo, Mn, Nb and Ta; and optionally (3) a third catalyst comprising a third inorganic oxide supporting 0.01-5 weight %of a noble metal component alone
• an exhaust gas cleaner which comprises (1) a first catalyst comprising a first porous inorganic oxide supporting 0.2-15 weight %of at least one Ag component selected from Ag and Ag compounds; (2) a second catalyst which is a mixture of two or more of an Ni catalyst, an Ag catalyst and a Cu catalyst, said Ni catalyst comprising a second porous inorganic oxide supporting 0.5-30 weight %of one or more of Ni and Ni compounds, said Ag catalyst comprising a second porous inorganic oxide supporting 0.5-15 weight %of one or more of Ag and Ag compounds, and said Cu catalyst comprising a second porous inorganic oxide supporting 0.5-15 weight %of one or more of Cu and Cu compounds and optionally at least one component selected from 5 weight %or less of one or more of alkali metal elements, rare earth elements and oxides thereof and 30 weight %or less of one or more of oxides of W, V, Mo, Mn, Nb and Ta, and optionally (3) a third catalyst comprising a third porous inorganic oxide,
• a method for removing nitrogen oxides by reduction from an exhaust gas containing nitrogen oxides and oxygen in an amount larger than its stoichiometric amount relative to unburned components in said exhaust gas which comprises (1) disposing an exhaust gas cleaner as defined above in a flow path of the exhaust gas; (2) introducing into the exhaust gas at least one reducing agent selected from hydrocarbons and oxygen-containing organic compounds on an upstream side of the exhaust gas cleaner; and (3) bringing the resulting exhaust gas containing the reducing agent into contact with the exhaust gas cleaner at 150-600°C, thereby causing a reaction of the nitrogen oxides with the reducing agent to substantially remove the nitrogen oxides by reduction.
• the exhaust gas cleaner of the present invention may be basically in two forms.
• the exhaust gas cleaner of a first preferred form is obtained by coating on a cleaner substrate at least one catalyst comprising a powdery porous inorganic oxide carrying one or more catalytically active components.
• the exhaust gas cleaner of such a form may be also obtained by carrying the catalytically active components onto a porous inorganic oxide powder coated on a cleaner substrate.
• Preferable materials for the cleaner substrate include porous, heat-resistant ceramics having a large specific surface area such as ⁇ -alumina, titania, zirconia and their composite oxides such as ⁇ -alumina-titania, ⁇ -alumina-silica, ⁇ -alumina-zirconia, titania-zirconia, etc. and oxide mixtures containing alumina. When a high heat resistance is required, cordierite, mullite, alumina or its composite oxides are preferable.
• the cleaner substrate may be formed from a known metal material.
• the shape and size of the cleaner substrate may be changed depending on applications.
• the cleaner substrate may be fabricated from two parts or more such as an inlet portion, an intermediate portion, an outlet portion, etc.
• the cleaner substrate may be of a three-dimensional structure such as a honeycomb, a foam, a refractory fiber assembly, etc. Further, the cleaner substrate may be of granules or pellets.
• Each of the catalysts may be coated on different portions of the same cleaner substrate, or each catalyst may be coated on separate cleaner substrates, and thereafter, fabricated into an exhaust gas cleaner.
• the catalyst may be coated on the cleaner substrate by a wash-coating method, a powder method, etc.
• a cleaner substrate having a catalyst on its surface may be produced by supporting, by a known impregnation method, a precipitation method, an ion-exchanging method, etc., the active component on a porous inorganic oxide coated on the cleaner substrate by a wash-coating method, sol-gel method, etc.
• the exhaust gas cleaner of a second preferred form may be produced by charging into a suitable reactor such as a catalytic converter, which is equipped with at least inlet and outlet portions, each of the catalysts obtained by carrying one or more catalytically active components on a pelletized, granular or powdery porous inorganic oxide, or obtained by forming a porous inorganic oxide carrying one or more catalytically active components into pellet, granule or powder.
• a suitable reactor such as a catalytic converter, which is equipped with at least inlet and outlet portions, each of the catalysts obtained by carrying one or more catalytically active components on a pelletized, granular or powdery porous inorganic oxide, or obtained by forming a porous inorganic oxide carrying one or more catalytically active components into pellet, granule or powder.
• the weight percentage of the catalytically active component is expressed by metal basis and based on the amount of porous inorganic oxide on which the component concerned is carried.
• the first preferred embodiment of the exhaust gas cleaner comprises (1) a first catalyst comprising a first porous inorganic oxide supporting an Ag component, (2) a second catalyst comprising a second porous inorganic oxide supporting an Ni component or two or more of Ag component, Cu component and Ni component, and optionally (3) a third catalyst comprising a third porous inorganic oxide supporting a noble metal component alone or in combination with a base metal component.
• the second catalyst may further support thereon at least one component selected from an alkali metal component, a rare earth component and a base metal component.
• the first, second and third catalyst are disposed in this order from the inlet side to the outlet side of the exhaust gas cleaner.
• the second catalyst When the second catalyst is one carrying two or more of Ag component, Cu component and Ni component, the second catalyst may be physically mixed with the third catalyst to for a mixed catalyst.
• the first catalyst is disposed on the inlet side and the mixed catalyst of the second and third catalysts is disposed on the outlet side.
• the first catalyst which is concerned in the reduction of nitrogen oxides in a wide temperature range, comprises a first porous inorganic oxide supporting at least one Ag component selected from Ag and Ag compounds.
• the first porous inorganic oxide may be at least one heat-resistant porous ceramic having a large specific surface area selected from the group consisting of alumina, titania, zeolite and composite oxides thereof, and preferably at least one of alumina and alumina-based composite oxides.
• Zeolite may include ferrierite, mordenite, ZSM-5, etc.
• Silica and titania may be contained in the composite oxides.
• Oxide mixtures of alumina containing titania, silica, zeolite, etc. may be preferably used.
• the alumina content in an alumina-based composite oxide or an oxide mixture containing alumina is preferred to be 50 weight %or more.
• the alumina-based composite oxide or the oxide mixture containing alumina improves durability and heat resistance of a catalyst even in the presence of sulfur dioxide in exhaust gas.
• the specific surface area of the first porous inorganic oxide is preferably 10 m 2 /g or more, and more preferably 30 m 2 /g or more.
• the Ag component may not be dispersed sufficiently throughout the porous inorganic oxide, failing to remove nitrogen oxides efficiently.
• the Ag component is at least one of Ag and Ag compounds which may include oxides of Ag, halides of Ag, sulfates of Ag and phosphates of Ag.
• Preferred Ag components are Ag, oxides of Ag, silver chloride and silver sulfate, and more preferred are Ag, oxides of Ag and silver chloride.
• the amount (silver element basis) of the Ag component supported on the first porous inorganic oxide is 0.2-15 weight %, and preferably 0.5-12 weight %.
• the amount is less than 0.2 weight %, the removal ratio of the nitrogen oxides may be low.
• an amount exceeding 15 weight % may decrease the NOx removal ratio because the reducing agent such as hydrocarbons and oxygen-containing organic compounds is likely to be predominantly burnt.
• the Ag component may be carried on the first porous inorganic oxide by known methods such as an impregnation method, a precipitation method, etc.
• the active component may be carried thereon also by an ion-exchanging method.
• Ag and/or Ag oxides may be carried by immersing the first porous inorganic oxide into an aqueous or ammoniacal aqueous solution of silver nitrate, silver acetate, etc., drying at about 50-150°C, preferably at about 70°C,and then subjecting the dried product to calcination by heating it stepwise from about 100°C to about 600°Cin air, nitrogen gas stream containing oxygen or hydrogen gas stream.
• the calcined product is preferred to be subjected to oxidation treatment at 300-650°C
• Silver sulfate may be carried, for example, by immersing the first porous inorganic oxide in a solution of silver sulfate in aqueous nitric acid or by immersing the first porous inorganic oxide in a solution of ammonium sulfate after immersing in an aqueous solution of silver nitrate, and then followed by the same drying and calcination steps as described above.
• Silver phosphate may be carried, for example, by immersing the porous inorganic oxide in an aqueous solution of silver nitrate while adding little by little phosphoric acid or ammonium phosphate under stirring. The mixture is further stirred for 4 hours while shielding the light. After drying, the resulting porous inorganic oxide is calcined at 120°C for one hour, 450°C for 3 hours to obtain a porous inorganic oxide carrying silver phosphate, and finally calcined at 600°C for 3 hours.
• the porous inorganic oxide impregnated with an aqueous solution of silver nitrate, etc. may be further immersed in an aqueous solution of ammonium halide to convert the silver nitrate into silver halide precipitation, and then followed by the same drying and calcination steps as described above.
• the average diameter, determined arithmetically, of the aggregate may be 10-10000 nm, preferably 10-5000 nm, and more preferably 10-2000 nm. Generally the smaller the average diameter of the aggregate, the higher the activity of the Ag catalyst. However, when the average diameter is less than 10 nm, the reducing agent (hydrocarbons and/or oxygen-containing organic compounds) may be predominantly oxidized, resulting in a decrease in the removal ratio of nitrogen oxides. On the other hand, when the average diameter is larger than 10000 nm, the catalytic activity of the Ag component may become low, resulting in a low removal ratio of nitrogen oxides.
• the second catalyst comprises a second porous inorganic oxide supporting an Ni component or two or more of Ag component, Cu component and Ni component.
• the second porous inorganic oxide may be at least one heat-resistant porous ceramic having a large specific surface area selected from the group consisting of alumina, silica, titania, zirconia, zeolite and composite oxides thereof.
• the specific surface area is preferably 10 m 2 /g or more.
• the Ni component is at least one of Ni and Ni compounds which may include oxides of Ni, halides of Ni and sulfates of Ni.
• the amount (nickel element basis) of the Ni component is 1-30 weight %, preferably 1-25 weight %.
• the Cu component is at least one of Cu and Cu compounds which may include oxides of Cu,halides of Cu and sulfates of Cu.
• the amount (silver, copper and nickel elements basis) of two or more of the Ag, Cu and Ni components is 1-30 weight %, preferably 1-25 weight %.
• the weight ratio (element basis) of Ni:Ag, Ni:Cu and Ag:Cu are preferably 1:5 to 5:1.
• the second catalyst may further carry the optional component selected from an alkali metal component, a rare earth component and a base metal component.
• the alkali metal component is at least one of alkali metal elements such as Na, K, etc. and oxides thereof.
• the rare earth component is at least one of rare earth elements such as La, Ce, etc. and oxides thereof.
• the amount (alkali metal and rare earth element basis) of the total of the alkali metal component and the rare earth component is 5 weight %or less, preferably 4 weight %or less.
• the base metal component is at least one of oxides of W, V, Mo, Mn, Nb and Ta.
• the amount (base metal element basis) is 30 weight %or less, preferably 24 weight %or less.
• the reduction of nitrogen oxides by ammonia produced on the first catalyst may be promoted by carrying this component.
• the above components may be carried on the second porous inorganic oxide by known methods such as an impregnation method, a precipitation method, etc.
• the active component may be carried thereon also by an ion-exchanging method.
• the Ag component may be carried by the same method as in the first catalyst.
• the other components may be carried basically in the same manner as in the preparation of the first catalyst.
• a second porous inorganic oxide impregnated with one or more of the components may then be subjected to the same drying and calcination steps as in the preparation of the first catalyst.
• the Ni component may be carried, for example, by immersing the second porous inorganic oxide in a solution containing the Ni component, such as aqueous solution of nickel nitrate, nickel sulfate, nickel chloride, etc.
• the Cu component may be carried, for example, by immersing the second porous inorganic oxide in a solution containing the Cu component, such as aqueous solution of copper sulfate, copper nitrate, copper acetate, copper chloride, etc.
• the alkali metal component may be carried, for example, by immersing the second porous inorganic oxide in an aqueous solution of nitrates, etc. of the alkali metal.
• the rare earth component may be carried, for example, by immersing the second porous inorganic oxide in a solution containing the rare earth component, such as aqueous solution of nitrate, etc. of rare earth element.
• the base metal component may be carried basically in the same manner as in the preparation of the first catalyst.
• the second porous inorganic oxide carrying the Ni component, etc. may be immersed in a solution containing the base metal component, such as aqueous solution of ammonium salt, etc. of W, V, Mo, Mn, Nb and Ta, and subjected to the same drying and calcination steps as in the preparation of the first catalyst, thereby carrying oxide of the above element.
• Titania carrying the W component may be prepared by using metatitanic acid (hydrated titanium oxide) as the starting material in place of titania.
• the weight ratio of the first catalyst and the second catalyst may be 1:10 to 20:1, preferably 1:10 to 10:1, and more preferably 1:5 to 10:1.
• the optional third catalyst comprises a third porous inorganic oxide supporting a noble metal component alone or in combination with a base metal component, and may be mixed with the second catalyst carrying two or more of Ag component, Cu component and Ni component.
• the third catalyst is disposed at the outlet side of the exhaust gas cleaner and is concerned in the reduction of NOx at a relatively low temperature and the oxidation of carbon monoxide, hydrocarbons and SOF.
• the third catalyst carrying both the noble metal component and base metal component may prevent the oxidation of sulfur dioxide.
• the third porous inorganic oxide may be at least one porous and heat-resistant ceramic selected from alumina, titania, zirconia, silica, zeolite and composite oxides thereof.
• the specific surface area is preferably 10 m 2 /g or more.
• the noble metal component is one or more of Pt, Pd, Ru, Rh, Ir and Au, and one or more of Pt, Pd, Ru, Rh and Au is preferable. At least one of Pt, Pd and Au is more preferred.
• the amount (noble metal element basis) to be supported on the third porous inorganic oxide is 0.01-5 weight %,and preferably 0.01-4 weight %. The amount more than 5 weight % may give no additional improvement in the removal efficiency.
• the base metal component is at least one of oxides of W, V, Mo, Mn, Nb and Ta.
• the amount (base metal element basis) to be supported is 0.2-10 weight %,preferably 0.2-9 weight %.
• the noble metal component may be carried on the third porous inorganic oxide basically in the same manner as in the preparation of the first catalyst.
• the third porous inorganic oxide may be immersed in a solution containing the noble metal component, such as aqueous solution of chloroplatinic acid, chloroauric acid, palladium chloride, etc., and subjected to the same drying and calcination steps as in the preparation of the first catalyst.
• the Pt component may exist either in the form of element or oxide at working temperatures at which the cleaner is used.
• the base metal component may be carried in the same manner as described in the second catalyst.
• the weight ratio (element basis) of the first catalyst and the third catalyst may be 1:5 to 20:1, preferably 1:4 to 10:1.
• the ratio is less than 1:5 (excess of the third catalyst)
• a sufficiently high removal ratio of the nitrogen oxides may not be achieved in a wide temperature range of 150-600°C.
• the ratio is higher than 20:1 (excess of the first catalyst)
• hydrocarbons, carbon monoxide and SOF may remain not oxidized.
• the weight ratio (element basis) of the second catalyst and the third catalyst is preferably 1:1 to 200:1, more preferably 1:1 to 100:1.
• the ratio is less than 1:1 (excess of the third catalyst)
• a sufficiently high removal ratio of the nitrogen oxides may not be achieved in a wide temperature range of 150-600°C.
• the ratio is higher than 20:1 (excess of the second catalyst)
• hydrocarbons, carbon monoxide and SOF may remain not oxidized.
• the second preferred embodiment of the exhaust gas cleaner comprises (1) a mixed catalyst of a first catalyst comprising a first porous inorganic oxide supporting an Ag component and a second catalyst comprising a second porous inorganic oxide supporting an Ni component alone or in combination with a Cu component, and optionally (2) a third catalyst comprising a third porous inorganic oxide supporting a noble metal component alone or in combination with a base metal component.
• the second catalyst may further support thereon at least one component selected from an alkali metal component, a rare earth component and a base metal component.
• the mixed catalyst of the first and second catalyst is disposed on the inlet side, and the third catalyst on the outlet side of the exhaust gas cleaner.
• the first catalyst of the second preferred embodiment which comprises the first porous inorganic oxide carrying the 0.2-15 weight %of the Ag component, is the same as the first catalyst of the first preferred embodiment.
• the second catalyst comprises a second inorganic oxide supporting 0.5-30 weight %,preferably 1-25 weight % of an Ni component alone or in combination with 0.5-30 weight %,preferably 1-25 weight %of a Cu component.
• the third catalyst is the same as the third catalyst of the first exhaust gas cleaner.
• the third preferred embodiment of the exhaust gas cleaner comprises (1) a first catalyst comprising a first porous inorganic oxide supporting an Ag component, (2) a second catalyst which is a mixture of two or more of an Ni catalyst comprising a second porous inorganic oxide supporting an Ni component, an Ag catalyst comprising a second porous inorganic oxide supporting an Ag component and a Cu catalyst comprising a second porous inorganic oxide supporting a Cu component and optionally at least one component selected from an alkali metal component, a rare earth component and a base metal component, and optionally (3) a third catalyst comprising a third porous inorganic oxide supporting a noble metal component alone or in combination with a base metal component.
• the first, second and third catalyst are disposed in this order from the inlet side to the outlet side of the exhaust gas cleaner.
• the second catalyst may be physically mixed with the third catalyst to form a mixed catalyst.
• the first catalyst of the third preferred embodiment is the same as the first catalyst of the first preferred embodiment.
• the second catalyst of the third preferred embodiment is a mixture of two or more of an Ni catalyst comprising a second porous inorganic oxide supporting an Ni component, an Ag catalyst comprising a second porous inorganic oxide supporting an Ag component and a Cu catalyst comprising a second porous inorganic oxide supporting a Cu component.
• the second porous inorganic oxide is the same as the second porous inorganic oxide of the first exhaust cleaner.
• the Ni component is at least one component selected from Ni and Ni compounds which may include oxides of Ni, halides of Ni, sulfates of Ni, etc., and is supported in an amount (nickel element basis) of 0.5-30 weight %,preferably 0.5-25 weigh %.
• the Ag component is at least one component selected from Ag and Ag compounds which may include oxides of Ag, halides of Ag, sulfates of Ag, phosphates of Ag, etc., and is supported in an amount (silver element basis) of 0.5-15 weight %,preferably 1-12 weight %.
• the Cu component is at least one component selected from the group consisting of Cu and Cucompounds which may include oxides of Cu, halides of Cu, sulfates of Cu, etc., and is supported in an amount (copper element basis) of 0.5-3 0 weight %, preferably 0.5-25 or 0.5-15 weight %.
• the Cu catalyst may further support the optional component selected from an alkali metal component, a rare earth component and a base metal component as in the case of the second catalyst of the first exhaust gas cleaner.
• the above catalyst may be prepared in accordance with the methods for preparing the second catalyst of the first exhaust cleaner.
• These catalysts may be mixed so that the weight ratio (element basis) of the catalysts, i.e., Ni catalyst:Ag catalyst, Ni catalyst:Cu catalyst and Ag catalyst:Cu catalyst, may be 1:5 to 5:1.
• the weight ratio (element basis) of the first catalyst and the second catalyst may be 1:10 to 20:1, preferably 1:5 to 10:1.
• the third catalyst is the same as the third catalyst of the first exhaust gas cleaner.
• the weight ratio (element basis) of the first catalyst and the third catalyst may be 1:5 to 20:1, preferably 1:4 to 10:1.
• the ratio is less than 1:5 (excess of the third catalyst)
• a sufficiently high removal ratio of the nitrogen oxides may not be achieved in a wide temperature range of 150-600°C.
• the ratio is higher than 20:1 (excess of the first catalyst)
• hydrocarbons, carbon monoxide and SOF may remain not oxidized.
• the second catalyst may be physically mixed with the third catalyst to form a mixed catalyst.
• the mixing ratio (element basis) of the second catalyst and the third catalyst is preferably 1:1 to 200:1, preferably 1:1 to 100:1 by weight.
• the ratio is less than 1:1 (excess of the third catalyst)
• a sufficiently high removal ratio of the nitrogen oxides may not be achieved in a wide temperature range of 150-600°C.
• the ratio is higher than 20:1 (excess of the second catalyst)
• hydrocarbons, carbon monoxide and SOF may remain not oxidized.
• Each of the catalysts described above may be coated on a cleaner substrate as described above by known methods such as a wash-coating method, etc.
• the thickness of the Ag catalyst coated on the cleaner substrate is preferably up to 300 ⁇ m, though it is usually restricted by the difference in a thermal expansion coefficients between the catalyst and the cleaner substrate. With such thickness, it may be possible to prevent the cleaner from being broken by a thermal shock, etc. during NOx-removing operations.
• the amount of the respective catalyst coated onto a surface ofthe cleaner substrate is preferably 20-300 g/liter, more preferably 50-200 g/liter based on the cleaner substrate.
• the amount is less than 20 g/liter, a sufficient removal ratio of the nitrogen oxides may not be achieved.
• an amount more than 300 g/liter may give no additional increase in removal efficiency, but may result in a higher loss of pressure.
• NOx may be effectively removed even from exhaust gas containing about 10 % moisture at a wide temperature range of 150-600°C
• the exhaust gas usually contains residual hydrocarbons such as ethylene, propylene, etc. to some extent. Since the amounts of residual hydrocarbons may not be sufficient to reduce all nitrogen oxides in the exhaust gas, at least one reducing agent may be externally introduced into the exhaust gas.
• One site for introducing thereducing agent is an upstream side of the exhaust gas cleaner.
• the reducing agent to be added to exhaust gas may include hydrocarbons and oxygen-containing organic compounds having at least two carbon atoms.
• the reducing agent may be added together with a fuel such as gasoline, diesel oil, kerosene, etc.
• hydrocarbons examples include alkanes, alkenes and alkynes which may be gaseous or liquid at the normal state (25°C, 1 atm).
• the alkanes and alkenes are preferred to have 2 or more carbon atoms.
• the liquid hydrocarbons may be diesel oil, cetane, heptane, kerosene, gasoline, etc., and those having a boiling point of 50-350°Care preferable.
• the oxygen-containing organic compound having at least two carbon atoms may include alcohols having two or more of carbon atoms such as ethanol, isopropyl alcohol, etc.
• the weight ratio (the reducing agent externally added with or without the above fuel/nitrogen oxides in exhaust gas) is preferably 0.1-5. When the weight ratio is less than 0.1, the removal ratio of nitrogen oxides may not be improved. On the other hand, when the weight ratio is more than 5, fuel efficiency may be low.
• the apparent space velocity of the exhaust gas passing through each of the catalysts is preferably controlled.
• the apparent space velocity may be 150,000 h -1 or less, preferably 100,000 h -1 or less, while 200,000 h -1 or less, preferably 150,000 h -1 or less on the third catalyst and the mixed catalyst of the second and third catalysts.
• the exhaust gas passing through the exhaust gas cleaner where the reducing agent is reacted with nitrogen oxides is kept at 150-600°C preferably 2 0 0 - 5 5 0°C and more preferably 3 0 0 - 5 0 0°C.
• the temperature is lower than 150°C, the reduction of nitrogen oxides by the reducing agent may not be sufficiently carried out.
• the reducing agent may be burned before it reacts with the nitrogen oxides, failing to reduce the nitrogen oxides effectively.
• the weight percentage of the catalytically active component is expressed by metal basis based on the porous inorganic oxide on which the component concerned is carried.
• a commercially available silica/alumina powder (silica content: 5 weight %, specific surface area: 350 m 2 /g) was immersed in an aqueous solution of silver nitrate and then dried at 70°Cfor 2 hours. The dried powder was heated to 600°Cstepwise and calcined there for 5 hours in air to prepare a first catalyst carrying 3.1 weight %of silver.
• the first catalyst (0.26 g) was coated on a commercially available honeycomb cordierite filter (diameter: 20 mm, length: 8.3 mm, 400 cells/in 2 ), dried and then heated to 600°Cstepwise to be calcined to prepare a first cleaner part (Ag).
• a second cleaner part (Ni) coated with 0.26 g of a second catalyst carrying 10 weight %of nickel in the form of oxide was prepared in the same manner as above except for immersing a ⁇ -alumina powder (specific surface area: 200 m 2 /g) in an aqueous solution of nickel nitrate.
• An exhaust gas cleaner consisting of the first cleaner part on the inlet side and the second cleaner part on the outlet side was disposed in a reactor tube.
• a test gas having the composition shown in Table 1 was caused to pass through the reactor pipe at a flow rate of 3.48 liters per minute (the normal state: 25°C, 1 atm) while maintaining the test gas in the reactor tube at a temperature of 300- 600°C to reduce nitrogen oxides with ethanol.
• the apparent space velocity on each of the first and second catalysts was about 80,000 h -1 .
• the removal ratio was determined as follows. The concentration of nitrogen oxides in the effluent gas from the exhaust gas cleaner was measured by a chemiluminescence analyzer. The removal ratio was calculated according to the equation of (NOx (in) -NOx (out) / NOx( in ) x 100. The results are shown in Table 2.
• Table 1 Component Concentration Nitrogen monoxide 800 ppm Oxygen 10 volume % Ethanol 1560 ppm Sulfur dioxide 30 ppm Nitrogen Balance Water 10 volume % of the total volume of the above components
• a second cleaner part (Cu, Ni) coated with 0.26 g of a second catalyst carrying 10 weight %of copper in the form of oxide and 4.4 weight %of nickel in the form of oxide was prepared in the same manner as in Example 1 except for immersing ⁇ -alumina powder (specific surface area: 200 m 2 /g) in an aqueous solution dissolving copper sulfate and nickel nitrate.
• a first cleaner part (Ag) coated with 0.26 g of a first catalyst carrying 3.0 weight %of silver was prepared in the same manner as in Example 1 except for using ⁇ -alumina powder (specific surface area: 200 m 2 /g).
• ⁇ -alumina powder (specific surface area: 200 m 2 /g) was dried and calcined at 500°C. Further, silver was carried on the ⁇ -alumina powder thus obtained in the same manner as in Example 1 to prepare a second catalyst carrying 8 weight %of copper in the form of oxide and 1 weight % of silver. A second cleaner part (Ag, Cu) coated with 0.26 g of the second catalyst was prepared in the same manner as in Example 1.
• titania powder (specific surface area: 35 m 2 /g) was dried in air successively at 80°C, 100°C and 120°C each for 2 hours, and then heated from 120°C to 500°C over 5 hours and calcined there for 4 hours to carry 4.8 weight %of vanadium in the form of oxide.
• Example 2 copper sulfate and nickel sulfate were further carried in the same manner as in Example 1 while immersing for 20 minutes the titania powder in an aqueous solution dissolving copper sulfate and nickel sulfate to prepare a second catalyst (Cu, Ni, V) supporting 4.8 weight %of vanadium in the form of oxide, 4.5 weight %of copper in the form of sulfate and 3.0 weight %of nickel in the form of sulfate.
• a second cleaner part honeycomb cordierite filter, diameter: 20 mm, length: 13.2 mm, 400 cells/in 2 ) coated with 0.26 g the second catalyst was prepared in the same manner as in Example 1.
• zeolite powder (molar ratio (SiO 2 /Al 2 O 3 ):27, specific surface area: 230 m 2 /g) was dried in air successively at 80°C, 100°C and 120°C each for 2 hours, and then calcined while heating from 120°C to 400°C stepwise in a nitrogen stream containing 20 %of oxygen to prepare a second catalyst (Cu, Ag) supporting 4.1 weight % of copper in the form of oxide and 1 weight %of silver.
• a second cleaner part coated with 0.26 g of the second catalyst was prepared in the same manner as in Example 1.
• a titania powder (specific surface area: 35 m 2 /g) was dried in air at 80°C for 2 hours.
• the dried powder was calcined at 120°C for 2 hours in nitrogen stream, and further calcined at 200-400°C for one hour while heated stepwise.
• the powder thus calcined were heated from 50°C to 400°Cover 5 hours in nitrogen stream containing 4 %hydrogen to be calcined there for 4 hours, and further heated from 50°C to 500°C over 5 hours in nitrogen stream containing 10 % oxygen to be calcined there for 5 hours, thereby preparing a third catalyst (Pt) carrying 1 weight %of platinum.
• a third cleaner part coated with 0.26 g of the third catalyst was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the first cleaner part (Ag) of Example 3, the second cleaner part (Cu, Ag) and the third cleaner part (Pt) in this order from the inlet side to the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 2.
• the space velocity on each of the first, second and third catalyst was about 80,000 h -1 , respectively.
• titania powder supporting 1 weight %of platinum was prepared.
• oxide of vanadium was further carried in the same manner as in Example 4 to prepare a third catalyst (V, Pt) carrying 3.3 weight %of vanadium in the form of oxide and 1 weight %of platinum.
• a third cleaner part coated with 0.26 g of the third catalyst was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the first cleaner part (Ag) of Example 1, the second cleaner part (Ni, Cu) of Example 2 and the third cleaner part (V, Pt) in this order from the inlet side to the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 2.
• the space velocity on each of the first, second and third catalyst was about 80,000 h -1 , respectively.
• Example 3 An exhaust cleaner consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 8.3 mm, 400 cells/in 2 ) coated with 0.26 g of the first catalyst (Ag) of Example 3 was prepared in the same manner as in Example 1. The results of the same test as in Example 1 are shown in Table 2. The space velocity was about 80,000 h -1 .
• Examples 1-6 showed high removal efficiency of nitrogen oxides in a wide temperature range of exhaust gas.
• a first cleaner part coated with 0.26 g of a first catalyst (Ag) supporting 3.1 weight % of silver was prepared in the same manner as in Example 1.
• a second catalyst (Ni, Cu) supporting 4 weight %of nickel in the form of oxide and 10 weight %of copper in the form of oxide was prepared in the same manner as in Example 2.
• a second cleaner part coated with a mixed catalyst of 0.26 g of the second catalyst and 0.0065 g of the third catalyst (mixing ratio: 40:1) was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the first cleaner part (Ag) on the inlet side and the second cleaner part (mixture of (Cu, Ni) and Pt) on the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 3 together with the results of Comparative Example 1.
• the space velocity on each of the first and mixed catalysts was about 80,000 h -1 .
• a second catalyst (Ag, Cu) comprising zeolite powder (molar ratio (SiO 2 /Al 2 O 3 ): 27, specific surface area: 230 m 2 /g) supporting 1.0 weight % of silver and 4.1 weight %of copper was prepared in the same manner as in Example 5.
• vanadium oxide was further carried in the same manner as in Example 4 to prepare a third catalyst (V, Pt) carrying 1.0 weight %of platinum and 3.3 weight %of vanadium in the form of oxide.
• a second cleaner part coated with a mixed catalyst of 0.26 g of the second catalyst and 0.0065 g of the third catalyst (mixing ratio: 40:1) was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the first cleaner part (Ag) of Example 7 on the inlet side and the second cleaner part (mixture of (Ag, Cu) and (V, Pt)) on the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 3.
• the space velocity on each of the first and mixed catalysts was about 80,000 h -1 .
• a first cleaner part coated with 0.26 g of a first catalyst (Ag) comprising ⁇ -alumina powder (specific surface area: 200 m 2 /g) carrying 3.0 weight % of silver was prepared in the same manner as in Example 3.
• a second catalyst (Ag, Ni) comprising silica/alumina powder (silica content: 5 weight %, specific surface area: 350 m 2 /g) carrying 2.0 weight %of silver and 10 weight %of nickel in the form of oxide was prepared in the same manner as in Example 1 while using an aqueous solution of silver nitrate and nickel nitrate.
• a second cleaner part coated with a mixed catalyst of 0.26 g of the second catalyst and 0.0065 g of the third catalyst of Example 7 (mixing ratio: 40:1) was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the first cleaner part (Ag) on the inlet side and the second cleaner part (mixture of (Ag, Ni) and Pt) on the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 3.
• the space velocity on each of the first and mixed catalysts was about 80,000 h -1 .
• Examples 7-9 where the Ag catalyst and the mixed catalyst was combinedly used showed high removal efficiency of nitrogen oxides in a wide temperature range of exhaust gas.
• a first catalyst (Ag) comprising silica/alumina powder (silica content: 5 weight %,specific surface area: 350 m 2 /g) carrying 3.1 weight % of silver was prepared in the same manner as in Example 1.
• a second catalyst (Cu, Ni) comprising silica/alumina powder (silica content: 5 weight %, specific surface area: 350 m 2 /g) carrying 4.4 weight %of copper in the form of oxide and 7 weight %of nickel in the form of oxide was prepared also in the same manner as in Example 1.
• An exhaust gas cleaner consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 13.2 mm, 400 cells/in 2 ) coated with a mixed catalyst of 0.2 g of the first catalyst and 0.06 g of the second catalyst was prepared in the same manner as in Example 1.
• the exhaust gas cleaner was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 4.
• the space velocity was about 50,000 h -1 .
• a first catalyst (Ag) comprisingy-alumina powder (Specific surface area: 200 m 2 /g) carrying 3.0 weight %of silver was prepared in the same manner as in Example 3.
• a second catalyst (Ni, La, Cs) comprising ⁇ -alumina powder (specific surface area: 200 m 2 /g) carrying 7 weight %of nickel, 0.4 weight %of lanthanum and 0.4 weight %of cesium was prepared in the same manner as in Example 1 while using an aqueous solution of nickel nitrate, lanthanum nitrate and cesium nitrate.
• An exhaust gas cleaner consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 13.2 mm, 400 cells/in 2 ) coated with a mixed catalyst of 0.2 g of the first catalyst and 0.06 g of the second catalyst was prepared in the same manner as in Example 1.
• the exhaust gas cleaner was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 4.
• the space velocity was about 50,000 h -1 .
• a second catalyst (V, Cu, Ni) comprising titania powder (specific surface area: 35 m 2 /g) supporting 4.8 weight %of vanadium in the form of oxide, 4.5 weight %of copper in the form of sulfate and 2.5 weight % of nickel in the form of sulfate was prepared in the same manner as in Example 4.
• An exhaust gas cleaner consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 13.2 mm, 400 cells/in 2 ) coated with a mixed catalyst of 0.2 g of the first catalyst (Ag) of Example 11 and 0.06 g of the second catalyst was prepared in the same manner as in Example 1.
• the exhaust gas cleaner was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 4.
• the space velocity was about 50,000 h -1 .
• a cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 6.6 mm, 400 cells/in 2 ) coated with 0.26 g of a catalyst (Pt) comprising titania powder (specific surface area: 35 m 2 /g) carrying 1 weight %of platinum was prepared in the same manner as in Example 5.
• a catalyst Pt
• titania powder specific surface area: 35 m 2 /g
• An exhaust gas cleaner consisting of the cleaner (mixture of Ag and (Cu, Ni)) of Example 10 on the inlet side and the above cleaner part (Pt) on the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 4.
• the space velocity was about 50,000 h -1 on the mixed catalyst and 100,000 h -1 on the Pt catalyst.
• titania powder (specific surface area: 35 m 2 /g) supporting 1.0 weight %of platinum was prepared.
• oxide of vanadium was further carried in the same manner as in Example 4 to prepare a catalyst (V, Pt) carrying 3.3 weight % of vanadium in the form of oxide and 1.0 weight % of platinum.
• a cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 6.6 mm, 400 cells/in 2 ) coated with 0.26 g of the catalyst was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the cleaner (mixture of Ag and (Cu,Ni)) of Example 10 on the inlet side and the above cleaner part (V, Pt) on the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 4.
• the space velocity was about 50,000 h -1 on the mixed catalyst and 100,000 h -1 on the V,Pt catalyst.
• Example 11 An exhaust cleaner consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 6.6 mm, 400 cells/in 2 ) coated with 0.26 g of the first catalyst (Ag) of Example 11 was prepared in the same manner as in Example 1. The results of the same test as in Example 1 are shown in Table 4. The space velocity was about 100,000 h -1 .
• Examples 10-14 where the Ag catalyst and the catalyst carrying Ni or Ni+Cu was combinedly used showed high removal efficiency of nitrogen oxides in a wide temperature range of exhaust gas.
• a first cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 8.3 mm, 400 cells/in 2 ) coated with 0.26 g of a first catalyst (Ag) comprising silica/alumina powder (silica content: 5 weight %,specific surface area: 350 m 2 /g) supporting 3.1 weight %of silver was prepared in the same manner as in Example 1.
• Ni catalyst comprising ⁇ -alumina powder (specific surface area: 200 m 2 /g) carrying 10 weight %of nickel in the form of oxide
• a Cu catalyst comprising ⁇ -alumina powder (specific surface area: 200 m 2 /g) carrying 10 weight %of copper in the form of oxide were prepared in the same manner as in Example- 1 while using an aqueous solution dissolving either nickel nitrate or copper sulfate.
• a second cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 8.3 mm, 400 cells/in 2 ) coated with a mixed catalyst (second catalyst) containing 0.13 g of the Ni catalyst and 0.13 g the Cu catalyst was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the first cleaner part (Ag) on the inlet side and the second cleaner part (mixture of Ni and Cu) on the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 5 together with the results of Comparative Example 1.
• the space velocity on each of the first and mixed catalysts was about 80,000 h -1 .
• An Ag catalyst comprising ⁇ -alumina powder (specific surface area: 200 m 2 /g) carrying 4.0 weight %of silver was prepared in the same manner as in Example 3.
• a second cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 8.3 mm, 400 cells/in 2 ) coated with a mixed catalyst (second catalyst) containing 0.13 g of the Ag catalyst and 0.13 g the Cu catalyst of Example 15 was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the first cleaner part (Ag) of Example 15 on the inlet side and the second cleaner part (mixture of Ag and Cu) on the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 5.
• the space velocity on each of the first and mixed catalysts was about 80,000 h -1 .
• a first cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 8.3 mm, 400 cells/in 2 ) coated with 0.26 g of a first catalyst (Ag) comprising ⁇ -alumina powder (specific surface area: 200 m 2 /g) supporting 3.0 weight %of silver was prepared in the same manner as in Example 1.
• An Ag catalyst comprising silica/alumina powder (silica content: 5 weight %,specific surface area: 350 m 2 /g) carrying 4.0 weight %of silver, and an Ni catalyst comprising silica/alumina powder (silica content: 5 weight %,specific surface area: 350 m 2 /g) carrying 10 weight %of nickel in the form of oxide were prepared in the same manner as in Example 1 while using an aqueous solution dissolving either silver nitrate or nickel sulfate.
• a second cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 8.3 mm, 400 cells/in 2 ) coated with a mixed catalyst containing 0.13 g of the Ag catalyst and 0.13 g the Ni catalyst was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the first cleaner part (Ag) on the inlet side and the second cleaner part (mixture of Ag and Ni) on the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 5.
• the space velocity on each of the first and mixed catalysts was about 80,000 h -1 .
• a Cu catalyst comprising zeolite powder (molar ratio (SiO 2 /Al 2 O 3 ): 27, specific surface area: 230 m 2 /g) carrying 4.1 weight % of copper in the form of oxide was prepared in the same manner as in Example 5 while using an aqueous solution of copper acetate.
• an Ag catalyst comprising the same type of zeolite powder carrying 1 weight % of silver was prepared.
• a second cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 8.3 mm, 400 cells/in 2 ) coated with a mixed catalyst containing 0.13 g of the Ag catalyst and 0.13 g the Cu catalyst was prepared in the same manner as in Example 1.
• a third cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 8.3 mm, 400 cells/in 2 ) coated with 0.26 g of the third catalyst comprising titania powder (specific surface area: 35 m 2 /g) carrying 1 weight %of platinum was prepared in the same manner as in Example 5.
• An exhaust gas cleaner consisting of the first cleaner part (Ag) of Example 17, the second cleaner part (mixture of Ag and Cu) and the third cleaner part (Pt) in this order from the inlet side to the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 5.
• the space velocity on each of the first, second and third catalyst was about 80,000 h -1 , respectively.
• titania powder (specific surface area: 35 m 2 /g) supporting 1.0 weight %of platinum was prepared.
• oxide of vanadium was further carried in the same manner as in Example 4 to prepare a catalyst (V, Pt) carrying 3.3 weight % of vanadium in the form of oxide and 1.0 weight %of platinum.
• a cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 6.6 mm, 400 cells/in 2 ) coated with 0.26 g of the catalyst was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the first cleaner part (Ag) of Example 15, the second cleaner part (mixture of Ag and Cu) of Example 16 and the third cleaner part (V,Pt) in this order from the inlet side to the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 5.
• the space velocity on each of the first, second and third catalyst was about 80,000 h -1 , respectively.
• Examples 15-19 where the Ag catalyst and the mixed catalyst was combinedly used showed high removal efficiency of nitrogen oxides in a wide temperature range of exhaust gas.
• a second cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 8.3 mm, 400 cells/in 2 ) coated with a mixed catalyst of 0.26 g of the second catalyst (mixture of Ni and Cu) of Example 15 and 0.0065 g of the third catalyst (Pt) of Example 18 (mixing ratio: 40:1) was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the first cleaner (Ag) of Example 15 on the inlet side and the second cleaner part (Ni, Cu, Pt) on the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 6 together with the results of Comparative Example 1.
• the space velocity was about 80,000 h -1 on both the Ag catalyst and the mixed catalyst.
• a second cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 8.3 mm, 400 cells/in 2 ) coated with a mixed catalyst of 0.26 g of the second catalyst (mixture of Ag and Cu) of Example 16 and 0.0065 g of the third catalyst (V, Pt) of Example 19 (mixing ratio: 40:1) was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the first cleaner (Ag) of Example 15 on the inlet side and the second cleaner part (Ag, Cu, V, Pt) on the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 6.
• the space velocity was about 80,000 h -1 on both the Ag catalyst and the mixed catalyst.
• a second cleaner part consisting of a honeycomb cordierite filter (diameter: 20 mm, length: 8.3 mm, 400 cells/in 2 ) coated with a mixed catalyst of 0.26 g of the second catalyst (mixture of Ag and Ni) of Example 17 and 0.0065 g of the third catalyst (Pt) of Example 18 (mixing ratio: 40:1) was prepared in the same manner as in Example 1.
• An exhaust gas cleaner consisting of the first cleaner (Ag) of Example 17 on the inlet side and the second cleaner part (Ag, Ni, Pt) on the outlet side was disposed in a reactor tube.
• the results of the same test as in Example 1 are shown in Table 6.
• the space velocity was about 80,000 h -1 on both the Ag catalyst and the mixed catalyst.
• Examples 20-22 where the Ag catalyst and the mixed catalyst was combinedly used showed high removal efficiency of nitrogen oxides in a wide temperature range of exhaust gas.

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